CO2 recovery unit and CO2  recovery method

ABSTRACT

A CO 2  recovery unit includes an absorber that reduces CO 2  in flue gas ( 101 ) discharged from a combustion facility ( 50 ) by absorbing CO 2  by an absorbent, a regenerator that heats the absorbent having absorbed CO 2  to emit CO 2 , and regenerates and supplies the absorbent to the absorber, and a regenerating heater that uses steam ( 106 ) supplied from the combustion facility ( 50 ) for heating the absorbent in the regenerator and returns heated condensed water ( 106   a ) to the combustion facility ( 50 ). The CO 2  recovery unit further includes a condensed water/flue gas heat exchanger ( 57 ) that heats the condensed water ( 106   a ) to be returned from the regenerating heater to the combustion facility ( 50 ) by heat-exchanging the condensed water ( 106   a ) with the flue gas ( 101 ) in a flue gas duct ( 51 ) in the combustion facility ( 50 ).

FIELD

The present invention relates to a CO₂ recovery unit and a CO₂ recovery method for promoting energy savings.

BACKGROUND

The greenhouse effect by CO₂ (carbon dioxide) has been pointed out as one of the causes of the global warming, and there is an urgent need to take measures against it for protecting the global environment on a global scale. The generation source of CO₂ ranges over all human activities that burn fossil fuel, and thus demands for emission limitation on CO₂ are further increasing. Along with this trend, targeting for power generating facilities such as a thermal power plant that uses a large amount of fossil fuel, a method of reducing and recovering CO₂ in flue gas by bringing flue gas from a boiler into contact with an amine absorbent such as an amine compound solution has been intensively studied.

As a CO₂ recovery unit that recovers CO₂ from flue gas from a boiler or the like by using an absorbent, there has been known a CO₂ recovery unit that reduces CO₂ in flue gas by bringing flue gas into contact with a CO₂ absorbent in an absorber, heats the absorbent that has absorbed CO₂ in a regenerator so as to emit CO₂ and to regenerate the absorbent, and then returns the absorbent to the absorber and reuses the absorbent (see, for example, Patent Literature 1).

To separate and recover CO₂ in the regenerator, the absorbent needs to be heated in a reboiler, and thus steam of a predetermined pressure for heating needs to be supplied. Conventionally, it has been proposed to regenerate the steam by using a part of steam generated in a combustion facility such as a boiler in a power plant (see, for example, Patent Literature 2).

Steam supplied to the regenerator becomes condensed water after heating the absorbent that has absorbed CO₂, and is returned to a combustion facility and heated again.

CITATION LIST Patent Literatures

-   Patent Literature 1: Japanese Patent Application Laid-open No.     H5-245339 -   Patent Literature 2: Japanese Utility Model Laid-open Publication     No. H3-193116

SUMMARY Technical Problem

As described above, a CO₂ recovery unit is installed while being added to a combustion facility, and consumes thermal energy of the combustion facility. Therefore, there is a problem that energy efficiency of the combustion facility is lowered. For example, in the case of a power generating facility, thermal energy of the power generating facility is consumed, thereby lowering a power output thereof.

The present invention has been achieved in view of the above problems, and an object of the present invention is to provide a CO₂ recovery unit and a CO₂ recovery method that can improve energy efficiency.

Solution to Problem

According to an aspect of the present invention, an CO₂ recovery unit includes: an absorber that reduces CO₂ in flue gas discharged from a combustion facility by absorbing CO₂ by an absorbent; a regenerator that heats the absorbent having absorbed CO₂ to emit CO₂, and regenerates and supplies the absorbent to the absorber; a regenerating heater that uses steam supplied from the combustion facility for heating the absorbent in the regenerator and returns heated condensed water to the combustion facility; and a condensed water/flue gas heat exchanger that heats condensed water to be returned from the regenerating heater to the combustion facility by heat-exchanging the condensed water with flue gas in a flue gas duct in the combustion facility.

According to the CO₂ recovery unit, because condensed water returned from the regenerating heater to the combustion facility by the condensed water/flue gas heat exchanger is preheated, consumption energy in the combustion facility can be reduced, thereby enabling to improve energy efficiency in a plant in which the CO₂ recovery unit is applied.

Advantageously, in the CO₂ recovery unit, a condensed water/flue gas heat exchanging line for heat-exchanging between condensed water and flue gas is provided in middle of a condensed water line for returning condensed water from the regenerating heater to the combustion facility, and a bypass line for directly connecting the condensed water line without via the condensed water/flue gas heat exchanging line is provided.

According to the CO₂ recovery unit, for example, when there is a load variation in at least one of a plant in which the CO₂ recovery unit is applied and the CO₂ recovery unit, a heat exchange amount between condensed water and flue gas in the condensed water/flue gas heat exchanger can be adjusted by the bypass line. Accordingly, a stable operation can be performed even at the time of the load variation.

Advantageously, the CO₂ recovery unit further includes: a circulating water/flue gas heat exchanger that performs heat exchange between circulating water and flue gas in a flue gas duct in the combustion facility, at a downstream of flue gas of the condensed water/flue gas heat exchanger; and a circulating water/absorbent heat exchanger that performs heat exchange between an absorbent having absorbed CO₂ in the absorber and the circulating water before the absorbent reaches the regenerator.

According to the CO₂ recovery unit, the absorbent is heated before reaching the regenerator by using heat of flue gas. Therefore, an amount of steam required in the regenerating heater for heating the absorbent can be reduced. Accordingly, consumption energy in the combustion facility required for recovering CO₂ can be reduced, thereby enabling to improve energy efficiency in a plant in which the CO₂ recovery unit is applied.

Advantageously, the CO₂ recovery unit further includes an air preheater that preheats combustion air before reaching the combustion facility by waste heat discharged in a process of recovering CO₂.

According to the CO₂ recovery unit, combustion air is preheated by using waste heat discharged in the process of recovering CO₂. Therefore, the temperature of flue gas discharged from the combustion facility rises, thereby increasing a heat exchange amount in the condensed water/flue gas heat exchanger. As a result, the temperature of condensed water returned from the regenerating heater to the combustion facility rises, thereby enabling to reduce consumption energy in the combustion facility required for recovering CO₂, and to improve energy efficiency in a plant in which the CO₂ recovery unit is applied.

Advantageously, the CO₂ recovery unit further includes an air preheater that preheats combustion air before reaching the combustion facility by the condensed water before reaching the condensed water/flue gas heat exchanger.

According to the CO₂ recovery unit, combustion air is preheated by using condensed water before reaching the condensed water/flue gas heat exchanger. Therefore, the temperature of flue gas discharged from the combustion facility rises, thereby increasing the heat exchange amount in the condensed water/flue gas heat exchanger. As a result, the temperature of condensed water returned from the regenerating heater to the combustion facility rises, thereby enabling to reduce consumption energy in the combustion facility required for recovering CO₂, and to improve energy efficiency in a plant in which the CO₂ recovery unit is applied.

According to another aspect of the present invention, an CO₂ recovery method includes: a CO₂ absorbing step of reducing CO₂ in flue gas discharged from a combustion facility by absorbing CO₂ by an absorbent; an absorbent regenerating step of heating the absorbent having absorbed CO₂ to emit CO₂, and regenerating and supplying the absorbent to the CO₂ absorbing step; a regeneration heating step of using steam supplied from the combustion facility for heating the absorbent at the absorbent regenerating step and returning heated condensed water to the combustion facility, and reusing the regenerated absorbent at the CO₂ absorbing step; and a condensed water/flue gas heat exchanging step of heating condensed water to be returned to the combustion facility by heat-exchanging the condensed water with flue gas in a flue gas duct in the combustion facility.

According to the CO₂ recovery method, because condensed water returned from the regeneration heating step to the combustion facility by the condensed water/flue gas heat exchanging step is preheated, consumption energy in the combustion facility can be reduced, thereby enabling to improve energy efficiency in a plant in which the CO₂ recovery unit is applied.

Advantageously, the CO₂ recovery unit further includes a non-heat exchanging step of returning condensed water to the combustion facility without via the condensed water/flue gas heat exchanging step.

According to the CO₂ recovery method, for example, when there is a load variation in at least one of a plant in which the CO₂ recovery unit is applied and the CO₂ recovery unit, a heat exchange amount between condensed water and flue gas at the condensed water/flue gas heat exchanging step can be adjusted by the non-heat exchanging step. Accordingly, a stable operation can be performed even at the time of the load variation.

Advantageously, the CO₂ recovery unit further includes a circulating water/flue gas heat exchanging step of performing heat exchange between circulating water and flue gas in a flue gas duct in the combustion facility, at a downstream of flue gas of the condensed water/flue gas heat exchanging step; and a circulating water/absorbent heat exchanging step of performing heat exchange between an absorbent having absorbed CO₂ at the CO₂ absorbing step and the circulating water before performing the absorbent regenerating step.

According to the CO₂ recovery method, the absorbent is heated before performing the absorbent regenerating step by using heat of flue gas. Therefore, an amount of steam required for the regeneration heating step for heating the absorbent can be reduced. Accordingly, consumption energy in the combustion facility required for recovering CO₂ can be reduced, thereby enabling to improve energy efficiency in a plant in which the CO₂ recovery unit is applied.

Advantageously, the CO₂ recovery unit further includes an air preheating step of preheating combustion air before reaching the combustion facility by waste heat discharged in a process of recovering CO₂.

According to the CO₂ recovery method, combustion air is preheated by using waste heat discharged in the process of recovering CO₂. Therefore, the temperature of flue gas discharged from the combustion facility rises, thereby increasing a heat exchange amount at the condensed water/flue gas heat exchanging step. As a result, the temperature of condensed water returned from the regenerating heater to the combustion facility rises, thereby enabling to reduce consumption energy in the combustion facility required for recovering CO₂, and to improve energy efficiency in a plant in which the CO₂ recovery unit is applied.

Advantageously, the CO₂ recovery unit further includes an air preheating step of preheating combustion air before reaching the combustion facility by the condensed water before performing the condensed water/flue gas heat exchanging step.

According to the CO₂ recovery method, combustion air is preheated by using condensed water before reaching the condensed water/flue gas heat exchanging step. Therefore, the temperature of flue gas discharged from the combustion facility rises, thereby increasing the heat exchange amount at the condensed water/flue gas heat exchanging step. As a result, the temperature of condensed water returned from the regenerating heater to the combustion facility rises, thereby enabling to reduce consumption energy in the combustion facility required for recovering CO₂, and to improve energy efficiency in a plant in which the CO₂ recovery unit is applied.

Advantageous Effects of Invention

According to the present invention, consumption energy in a combustion facility is reduced and energy efficiency thereof can be improved.

BRIEF DESCRIPTION OF DRAWINGS

FIG. 1 is a schematic diagram of a plant in which a CO₂ recovery unit according to a first embodiment of the present invention is applied.

FIG. 2 is a schematic diagram of the CO₂ recovery unit according to the first embodiment of the present invention.

FIG. 3 is a schematic diagram of a plant in which a CO₂ recovery unit according to another mode of the first embodiment of the present invention is applied.

FIG. 4 is a schematic diagram of a plant in which a CO₂ recovery unit according to a second embodiment of the present invention is applied.

FIG. 5 is a schematic diagram of the CO₂ recovery unit according to the second embodiment of the present invention.

FIG. 6 is a schematic diagram of a plant in which a CO₂ recovery unit according to a third embodiment of the present invention is applied.

FIG. 7 is a schematic diagram of a plant in which a CO₂ recovery unit according to a fourth embodiment of the present invention is applied.

FIG. 8 depicts a power output reduction rate of a thermal power generating facility according to Examples of the present invention.

DESCRIPTION OF EMBODIMENTS

Embodiments of the present invention will be explained below in detail with reference to the accompanying drawings. The present invention is not limited to the embodiments. In addition, constituent elements in the embodiments include those that can be easily replaced or assumed by persons skilled in the art, or that are substantially equivalent.

[First Embodiment]

A first embodiment of the present invention is explained with reference to the drawings. FIG. 1 is a schematic diagram of a plant in which a CO₂ recovery unit according to the first embodiment is applied. FIG. 2 is a schematic diagram of the CO₂ recovery unit according to the first embodiment.

As shown in FIG. 1, a plant 5, for example, a power generation plant mainly includes a boiler that heats water in a sealed vessel by the thermal energy acquired by burning fuel, thereby acquiring high-temperature and high-pressure superheated steam, a combustion facility 50 including various turbines that acquire rotative power by superheated steam from the boiler, and a power generator (not shown) that generates power by the rotative power of a steam turbine. Although not shown in FIG. 1, the turbine includes a high pressure turbine, an intermediate pressure turbine, and a low pressure turbine. The plant 5 further includes a desulfurizer 52 that reduces sulfur content (including a sulfur compound) contained in flue gas 101 in a flue gas duct 51 for the passage of the flue gas 101 discharged from the boiler in the combustion facility 50, and a CO₂ recovery unit 53 that reduces CO₂ (carbon dioxide) contained in the flue gas 101 discharged from the boiler in the combustion facility 50. That is, a power generation plant as the plant 5 generates power by superheated steam from the boiler in the combustion facility 50, and discharges from a stack 54 emission gas 101 a, from which sulfur content and CO₂ discharged from the boiler in the combustion facility 50 are reduced.

In this type of plant 5, the boiler in the combustion facility 50 is provided with an air/flue gas heat exchanger 55. The air/flue gas heat exchanger 55 is provided while bridging an air line 56 that supplies combustion air 102 to the boiler in the combustion facility 50 and the flue gas duct 51, and performs heat exchange between the flue gas 101 discharged from the boiler and the combustion air 102 supplied to the boiler. The air/flue gas heat exchanger 55 improves the thermal efficiency of the boiler by preheating the combustion air 102 to the boiler.

As shown in FIG. 2, the CO₂ recovery unit 53 includes a cooling column 1 that cools the flue gas 101 discharged from the boiler in the combustion facility 50 by cooling water 103, an absorber 2 that causes a lean solution 104 a of an absorbent 104, which is an aqueous solution of an amine compound that absorbs CO₂, to be brought into countercurrent contact with the flue gas 101 to absorb CO₂ in the flue gas 101 by the absorbent 104 and discharges the emission gas 101 a from which CO₂ is reduced, and a regenerator 3 that emits CO₂ from a rich solution 104 b of the absorbent 104 having absorbed CO₂ to regenerate it to the lean solution 104 a, and returns the lean solution 104 a to the absorber 2.

In the cooling column 1, the flue gas 101 containing CO₂ is boosted by a flue gas blower (not shown) and fed into the cooling column 1, and is brought into countercurrent contact with the cooling water 103, thereby cooling the flue gas 101.

The cooling water 103 is accumulated in a lower portion of the cooling column 1, pressure-fed by a cooling-water circulating pump 1 a, and supplied to an upper portion of the cooling column 1 through a cooling water line 1 b. The cooling water 103 is then brought into countercurrent contact with the flue gas 101 moving upward at a position of a packed bed 1 d provided in a process leading to the lower portion of the cooling column 1, while flowing down from a nozzle 1 c provided in the upper portion of the cooling column 1. Furthermore, a cooler 1 e is provided in the cooling water line 1 b, and by cooling the cooling water 103 to a temperature lower than that of the flue gas 101, a part of moisture in the flue gas 101 condenses in the cooling column 1 to become condensed water. The flue gas 101 cooled in the cooling column 1 is discharged from a top portion of the cooling column 1 through a flue gas line 1 f and supplied to the absorber 2.

The absorber 2 has a CO₂ absorbing unit 21 in a lower portion thereof, and a water-washing unit 22 in an upper portion thereof. The CO₂ absorbing unit 21 brings the flue gas 101 supplied from the cooling column 1 into countercurrent contact with the lean solution 104 a of the absorbent 104, so that CO₂ in the flue gas 101 is absorbed by the absorbent 104 and reduced (CO₂ absorbing step).

The lean solution 104 a of the absorbent 104 is supplied from the regenerator 3, and brought into countercurrent contact with the flue gas 101 moving upward at a position of a packed bed 21 b provided in a process leading to the lower portion of the absorber 2, while flowing down from a nozzle 21 a, to become the rich solution 104 b having absorbed CO₂, and then accumulated at a bottom portion of the absorber 2. The rich solution 104 b of the absorbent 104 accumulated at the bottom portion of the absorber 2 is then pressure-fed by a rich-solution discharge pump 21 c positioned outside of the absorber 2, and supplied to the regenerator 3 through a rich solution line 21 d. Furthermore, in the process of being supplied to the regenerator 3 through the rich solution line 21 d, the rich solution 104 b of the absorbent 104 is heat-exchanged with the lean solution 104 a of the absorbent 104 in the process of being supplied to the absorber 2 through a lean solution line 31 d described later, by a rich/lean heat exchanger 4.

The water-washing unit 22 brings the emission gas 101 a, from which CO₂ is reduced by the CO₂ absorbing unit 21, into countercurrent contact with wash water 105 to reduce the amine compound entrained with the emission gas 101 a by the wash water 105, and discharges the emission gas 101 a, from which the amine compound is reduced, to outside of the absorber 2.

The wash water 105 is brought into countercurrent contact with the emission gas 101 a moving upward at a position of a packed bed 22 b provided in a process leading to the lower part of the absorber 2, while flowing down from a nozzle 22 a, and is accumulated in a water receiver 22 c. The wash water 105 accumulated in the water receiver 22 c is then pressure-fed by a wash-water discharge pump 22 d positioned outside of the absorber 2, cooled by a cooler 22 f, while being circulated through a wash water line 22 e, and caused to flow down from the nozzle 22 a again.

The regenerator 3 has an absorbent regenerating unit 31 in a lower half thereof. The absorbent regenerating unit 31 recovers CO₂ from the rich solution 104 b of the absorbent 104 and regenerates it as the lean solution 104 a, thereby emitting CO₂ from the absorbent 104 having absorbed CO₂ (absorbent regenerating step).

The rich solution 104 b of the absorbent 104 is supplied through the rich solution line 21 d of the CO₂ absorbing unit 21 in the absorber 2, and caused to flow down from a nozzle 31 a. The rich solution 104 b then becomes the lean solution 104 a, from which almost all CO₂ has been emitted, due to an endothermic reaction by a regenerating heater 32 connected to a lower portion of the regenerator 3, while passing through a lower-portion packed bed 31 b provided in a process leading to the lower portion of the regenerator 3, and accumulated at a bottom portion of the regenerator 3. Subsequently, in a process of being pressure-fed by a lean-solution discharge pump 31 c positioned outside of the regenerator 3, and supplied to the absorber 2 through the lean solution line 31 d, the lean solution 104 a accumulated at the lower portion of the regenerator 3 is heat-exchanged with the rich solution 104 b in the process of being supplied to the regenerator 3 through the rich solution line 21 d by the rich/lean heat exchanger 4, and cooled by a cooler 31 e.

Meanwhile, the emitted CO₂ moves upward in the regenerator 3, passes through an upper-portion packed bed 31 f, and discharged from a top portion of the regenerator 3. At this time, because moisture is contained in CO₂, by cooling CO₂ in a cooler 33 b, the moisture contained in CO₂ is condensed, and the condensed water and CO₂ are separated by a CO₂ separator 33 c. High-purity CO₂ separated from condensed water is emitted from a CO₂ emission line 33 d to outside of a system of a CO₂ recovery process, and used or dispensed with in subsequent steps. The condensed water is transported by a condensed water pump 33 e, a part of which is supplied from a nozzle 33 g at a top part of the regenerator 3 into the regenerator 3, through a regenerator reflux-water line 33 f.

The regenerating heater 32 heats the absorbent 104 accumulated at the bottom portion of the regenerator 3 by steam 106, in a circulating process for returning the absorbent 104 to the bottom portion of the regenerator 3, while extracting the absorbent 104 to outside of the regenerator 3 via a heating line 32 a. The steam 106 supplied to the regenerating heater 32 by a steam extracting line 32 b is condensed to become condensed water 106 a after heating the absorbent 104, and discharged via a condensed water line 32 c (regeneration heating step).

Furthermore, the absorbent regenerating unit 31 is provided with a lean solution/condensed water heat recovery unit 34. The lean solution/condensed water heat recovery unit 34 performs heat exchange among the extracted absorbent 104 and the lean solution 104 a of the absorbent 104 in a process of being supplied to the absorber 2 through the lean solution line 31 d and the condensed water 106 a in a process of being discharged through the condensed water line 32 c, in the circulating process for returning the absorbent 104 in the process of being regenerated in the absorbent regenerating unit 31 to the regenerator 3, while extracting the absorbent 104 to outside of the regenerator 3.

In the CO₂ recovery unit 53 described above, in the regenerating heater 32 (regeneration heating step), as shown in FIG. 1, the steam 106 supplied to the regenerating heater 32 is extracted from the combustion facility 50 in the plant 5 via the steam extracting line 32 b (the sign A in FIG. 1 and FIG. 2). Furthermore, in the CO₂ recovery unit 53, the condensed water 106 a after being used for heating the absorbent 104 in the regenerating heater 32 is returned to the boiler in the combustion facility 50 via the condensed water line 32 c (the sign B in FIG. 1 and FIG. 2). The condensed water 106 a to be returned to the boiler in the combustion facility 50 from the regenerating heater 32 in the CO₂ recovery unit 53 via the condensed water line 32 c is returned to the boiler in the combustion facility 50, while dissolved oxygen is removed by a deaerator (not shown).

As shown in FIG. 1, a condensed water/flue gas heat exchanging line 57 a is put in the condensed water line 32 c. The condensed water/flue gas heat exchanging line 57 a is extended to the flue gas duct 51 disposed between the air/flue gas heat exchanger 55 and the desulfurizer 52 to form a condensed water/flue gas heat exchanger 57 (condensed water/flue gas heat exchanging step) that heats the condensed water 106 a to be returned from the regenerating heater 32 to the combustion facility 50 by heat-exchanging the condensed water 106 a with the flue gas 101 in the flue gas duct 51.

As described above, the CO₂ recovery unit 53 according to the first embodiment includes the absorber 2 that reduces CO₂ in the flue gas 101 discharged from the combustion facility 50 by absorbing CO₂ by the lean solution 104 a of the absorbent 104, the regenerator 3 that heats the rich solution 104 b of the absorbent 104 having absorbed CO₂ to emit CO₂, and regenerates and supplies the absorbent to the absorber 2, and the regenerating heater 32 that uses the steam 106 supplied from the combustion facility 50 for heating the absorbent 104 in the regenerator 3 and returns the heated condensed water 106 a to the combustion facility 50. The CO₂ recovery unit further includes the condensed water/flue gas heat exchanger 57 that heats the condensed water 106 a to be returned from the regenerating heater 32 to the combustion facility 50 by heat-exchanging the condensed water 106 a with the flue gas 101 in the flue gas duct 51 in the combustion facility 50.

According to the CO₂ recovery unit 53, because the condensed water 106 a to be returned from the regenerating heater 32 to the combustion facility 50 is preheated by the condensed water/flue gas heat exchanger 57, consumption energy in the combustion facility 50 can be reduced, thereby enabling to improve energy efficiency in the plant 5 in which the CO₂ recovery unit 53 is applied.

FIG. 3 depicts another mode of the CO₂ recovery unit 53 according to the first embodiment. As shown in FIG. 3, a bypass line 57 b that directly connects the condensed water line 32 c without via the condensed water/flue gas heat exchanging line 57 a is provided in the condensed water line 32 c for returning the condensed water 106 a from the regenerating heater 32 to the combustion facility 50. Furthermore, an on-off valve 57 c is provided on an upstream side of the condensed water/flue gas heat exchanging line 57 a for feeding the condensed water 106 a to the condensed water/flue gas heat exchanger 57. Further, an on-off valve 57 d is provided in the bypass line 57 b.

When heat exchange between the condensed water 106 a and the flue gas 101 is performed in the condensed water/flue gas heat exchanger 57, the on-off valve 57 c is opened, and the on-off valve 57 d is closed. With this configuration, the condensed water 106 a in a process of being returned to the combustion facility 50 via the condensed water line 32 c passes through the condensed water/flue gas heat exchanging line 57 a. Therefore, heat exchange between the condensed water 106 a and the flue gas 101 is performed in the condensed water/flue gas heat exchanger 57.

On the other hand, when heat exchange between the condensed water 106 a and the flue gas 101 is not performed in the condensed water/flue gas heat exchanger 57, the on-off valve 57 c is closed, and the on-off valve 57 d is opened. With this configuration, the condensed water 106 a in the process of being returned to the combustion facility 50 via the condensed water line 32 c is returned to the combustion facility 50 without via the condensed water/flue gas heat exchanging line 57 a. Therefore, heat exchange between the condensed water 106 a and the flue gas 101 is not performed in the condensed water/flue gas heat exchanger 57 (non-heat exchanging step).

As described above, in the CO₂ recovery unit 53 according to the first embodiment, the condensed water/flue gas heat exchanging line 57 a for performing heat exchange between the condensed water 106 a and the flue gas 101 is provided in the middle of the condensed water line 32 c for returning the condensed water 106 a from the regenerating heater 32 to the combustion facility 50, and the bypass line 57 b for directly connecting the condensed water line 32 c without via the condensed water/flue gas heat exchanging line 57 a is provided.

According to the CO₂ recovery unit 53, for example, when there is a load variation in at least one of the plant 5 and the CO₂ recovery unit 53, the heat exchange amount between the condensed water 106 a and the flue gas 101 in the condensed water/flue gas heat exchanger 57 can be adjusted by the bypass line 57 b. Accordingly, a stable operation can be performed even at the time of the load variation.

A CO₂ recovery method according to the first embodiment includes a CO₂ absorbing step of reducing CO₂ in the flue gas 101 discharged from the combustion facility 50 by absorbing CO₂ by the rich solution 104 b of the absorbent 104, an absorbent regenerating step of heating the rich solution 104 b of the absorbent 104 having absorbed CO₂ to emit CO₂, and regenerating and supplying the absorbent to the CO₂ absorbing step, and a regeneration heating step of using the steam 106 supplied from the combustion facility 50 for heating the absorbent 104 at the absorbent regenerating step and returning the heated condensed water 106 a to the combustion facility 50. The CO₂ recovery method further includes a condensed water/flue gas heat exchanging step of heating the condensed water 106 a to be returned to the combustion facility 50 by heat-exchanging the condensed water 106 a with the flue gas 101 in the flue gas duct 51 in the combustion facility 50.

According to the CO₂ recovery method, because the condensed water 106 a to be returned from the regeneration heating step to the combustion facility 50 is preheated by the condensed water/flue gas heat exchanging step, consumption energy in the combustion facility 50 can be reduced, thereby enabling to improve energy efficiency in the plant 5 in which the CO₂ recovery method is applied.

Furthermore, the CO₂ recovery method according to the first embodiment includes a non-heat exchanging step of returning the condensed water 106 a to the combustion facility 50 without via the condensed water/flue gas heat exchanging step.

According to the CO₂ recovery method, for example, when there is a load variation in at least one of the plant 5 and the CO₂ recovery unit 53, the heat exchange amount between the condensed water 106 a and the flue gas 101 at the condensed water/flue gas heat exchanging step can be adjusted by the non-heat exchanging step. Accordingly, a stable operation can be performed even at the time of the load variation.

[Second Embodiment]

A second embodiment of the present invention is explained with reference to the drawings. FIG. 4 is a schematic diagram of a plant in which a CO₂ recovery unit according to a second embodiment is applied, and FIG. 5 is a schematic diagram of the CO₂ recovery unit according to the second embodiment.

The CO₂ recovery unit 53 according to the present embodiment includes the condensed water/flue gas heat exchanger 57 (in a CO₂ recovery method, condensed water/flue gas heat exchanging step), similarity to the CO₂ recovery unit 53 according to the first embodiment. The CO₂ recovery unit 53 further includes a circulating water/flue gas heat exchanger 58 a (in the CO₂ recovery method, circulating water/flue gas heat exchanging step) and a circulating water/absorbent heat exchanger 58 b (in the CO₂ recovery method, circulating water/absorbent heat exchanging step). Therefore, in the second embodiment, a configuration related to the circulating water/flue gas heat exchanger 58 a (in the CO₂ recovery method, circulating water/flue gas heat exchanging step) and the circulating water/absorbent heat exchanger 58 b (in the CO₂ recovery method, circulating water/absorbent heat exchanging step) is explained, and elements equivalent to those in the first embodiment described above are denoted by like reference signs and explanations thereof will be omitted.

As shown in FIG. 4, the circulating water/flue gas heat exchanger 58 a is provided in the flue gas duct 51 in a downstream of the flue gas 101 of the condensed water/flue gas heat exchanger 57. More specifically, the circulating water/flue gas heat exchanger 58 a is provided between the condensed water/flue gas heat exchanger 57 and the desulfurizer 52 in the flue gas duct 51. The circulating water/flue gas heat exchanger 58 a is supplied with circulating water 107 by a circulating water line 58 c.

As shown in FIG. 5, the circulating water/absorbent heat exchanger 58 b is provided in the rich solution line 21 d for supplying the rich solution 104 b of the absorbent 104 having absorbed CO₂ in the absorber 2 to the regenerator 3. More specifically, the circulating water/absorbent heat exchanger 58 b is provided between the rich/lean heat exchanger 4 and the regenerator 3 in the rich solution line 21 d. The circulating water 107 is supplied to the circulating water/absorbent heat exchanger 58 b by the circulating water line 58 c. That is, the circulating water 107 is circulated by the circulating water line 58 c through the circulating water/flue gas heat exchanger 58 a and the circulating water/absorbent heat exchanger 58 b.

Meanwhile, in the circulating water/flue gas heat exchanger 58 a (circulating water/flue gas heat exchanging step), the circulating water 107 circulated by the circulating water line 58 c (the signs C and D in FIGS. 4 and 5) is heated by-heat exchanging the circulating water 107 with the flue gas 101 in the flue gas duct 51 in the combustion facility 50. Furthermore, in the circulating water/absorbent heat exchanger 58 b (circulating water/absorbent heat exchanging step), the rich solution 104 b of the absorbent 104 having absorbed CO₂ in the absorber 2 is heated by heat-exchanging the rich solution 104 b with the circulating water 107 circulated by the circulating water line 58 c (the signs C and D in FIGS. 4 and 5).

As described above, the CO₂ recovery unit 53 according to the present embodiment includes the circulating water/flue gas heat exchanger 58 a that heats the circulating water 107 by heat-exchanging it with the flue gas 101 in the flue gas duct 51 in the combustion facility 50 in the downstream of the flue gas 101 of the condensed water/flue gas heat exchanger 57, and the circulating water/absorbent heat exchanger 58 b that heats the rich solution 104 b of the absorbent 104 having absorbed CO₂ in the absorber 2 by heat-exchanging the rich solution 104 b with the circulating water 107 before reaching the regenerator 3.

According to the CO₂ recovery unit 53, the rich solution 104 b of the absorbent 104 is heated before reaching the regenerator 3 by using the heat of the flue gas 101. Therefore, an amount of steam required by the regenerating heater 32 for heating the rich solution 104 b of the absorbent 104 can be reduced, and thus consumption energy in the combustion facility 50 required for recovering CO₂ can be reduced, thereby enabling to improve energy efficiency in the plant 5 in which the CO₂ recovery unit 53 is applied.

As shown in FIG. 4, in the CO₂ recovery unit 53 according to the second embodiment, an on-off valve 58 d can be provided in the circulating water line 58 c for circulating the circulating water 107. When the on-off valve 58 d is opened, the circulating water 107 is circulated, thereby performing heat exchange between the circulating water 107 and the flue gas 101, and between the rich solution 104 b of the absorbent 104 and the circulating water 107. On the other hand, when the on-off valve 58 d is closed, the circulating water 107 is not circulated. Therefore, the circulating water 107 and the flue gas 101 are not heat-exchanged, and the rich solution 104 b of the absorbent 104 and the circulating water 107 are not heat-exchanged.

According to the CO₂ recovery unit 53, for example, when there is a load variation in at least one of the plant 5 and the CO₂ recovery unit 53, the heat exchange amount in the circulating water/flue gas heat exchanger 58 a and the circulating water/absorbent heat exchanger 58 b can be adjusted by operating the on-off valve 58 d. Accordingly, a stable operation can be performed even at the time of the load variation.

The CO₂ recovery method according to the second embodiment includes a circulating water/flue gas heat exchanging step of heating the circulating water 107 by heat-exchanging it with the flue gas 101 in the flue gas duct 51 in the combustion facility 50 in the downstream of the flue gas 101 at the condensed water/flue gas heat exchanging step, and a circulating water/absorbent heat exchanging step of heating the rich solution 104 b of the absorbent 104 having absorbed CO₂ at a CO₂ absorbing step by heat-exchanging the rich solution 104 b with the circulating water 107 before performing an absorbent regenerating step.

According to the CO₂ recovery method, the rich solution 104 b of the absorbent 104 is heated by using the heat of the flue gas 101 before performing the absorbent regenerating step. Therefore, an amount of steam required by a regeneration heating step for heating the rich solution 104 b of the absorbent 104 can be reduced, and thus consumption energy in the combustion facility 50 required for recovering CO₂ can be reduced, thereby enabling to improve energy efficiency in the plant 5 in which the CO₂ recovery method is applied.

As shown in FIG. 4, the CO₂ recovery method according to the second embodiment further includes a non-heat exchanging step of stopping the heat exchange at the circulating water/flue gas heat exchanging step and the circulating water/absorbent heat exchanging step by closing the on-off valve 58 d.

According to the CO₂ recovery method, for example, when there is a load variation in at least one of the plant and the CO₂ recovery unit 53, the heat exchange amount at the circulating water/flue gas heat exchanging step and the circulating water/absorbent heat exchanging step can be adjusted by operating the on-off valve 58 d. Accordingly, a stable operation can be performed even at the time of the load variation.

In FIG. 4, which explains the present embodiment, a configuration including the circulating water/flue gas heat exchanger 58 a (circulating water/flue gas heat exchanging step) and the circulating water/absorbent heat exchanger 58 b (circulating water/absorbent heat exchanging step) is shown with respect to the configuration shown in FIG. 3, which explains the first embodiment. However, the circulating water/flue gas heat exchanger 58 a (circulating water/flue gas heat exchanging step) and the circulating water/absorbent heat exchanger 58 b (circulating water/absorbent heat exchanging step) can be provided in the configuration shown in FIG. 1, which explains the first embodiment.

[Third Embodiment]

A third embodiment of the present invention is explained with reference to the drawings. FIG. 6 is a schematic diagram of a plant in which a CO₂ recovery unit according to the third embodiment is applied.

The CO₂ recovery unit 53 according to the present embodiment includes the condensed water/flue gas heat exchanger 57 (in a CO₂ recovery method, condensed water/flue gas heat exchanging step), similarity to the CO₂ recovery unit 53 according to the first embodiment. The CO₂ recovery unit 53 further includes an air preheater 59 (in the CO₂ recovery method, air preheating step). Therefore, in the third embodiment, a configuration of the air preheater 59 (in the CO₂ recovery method, air preheating step) is explained, and elements equivalent to those in the first embodiment described above are denoted by like reference signs and explanations thereof will be omitted.

As shown in FIG. 6, the air preheater 59 has a heat discharge line 59 a. The heat discharge line 59 a is provided to circulate a heat medium 108 such as circulating water between the air line 56 in an upstream of air of the air/flue gas heat exchanger 55 and a cooler that discharges heat in a process of recovering CO₂ in the CO₂ recovery unit 53. As shown in FIG. 2 (or in FIG. 5), the cooler that discharges waste heat in the process of recovering CO₂ in the CO₂ recovery unit 53 includes at least one of the cooler 1 e provided in the cooling water line 1 b of the cooling column 1, the cooler 22 f provided in the wash water line 22 e of the absorber 2, the cooler 31 e provided in the lean solution line 31 d extending from the regenerator 3 to the absorber 2, and the cooler 33 b provided in a CO₂ emission line 33 a of a CO₂ recovering unit 33. That is, the heat medium 108 is circulated by the waste heat line 59 a through the air line 56 and the coolers 1 e, 22 f, 31 e, and 33 b.

Meanwhile, in the air preheater 59 (air preheating step), the combustion air 102 in the air line 56 is preheated by heat-exchanging the combustion air 102 with the heat medium 108 circulating through the waste heat line 59 a (the signs E and F in FIG. 2 (in FIG. 5) and FIG. 6).

As described above, the CO₂ recovery unit 53 according to the third embodiment includes the air preheater 59 that preheats the combustion air 102 before reaching the combustion facility 50 by waste heat discharged in the process of recovering CO₂.

According to the CO₂ recovery unit 53, the combustion air 102 is preheated by using waste heat discharged in the process of recovering CO₂. Therefore, the temperature of the flue gas 101 discharged from the boiler in the combustion facility 50 rises, thereby increasing the heat exchange amount in the condensed water/flue gas heat exchanger 57. As a result, the temperature of the condensed water 106 a returned from the regenerating heater 32 to the combustion facility 50 rises, thereby enabling to reduce consumption energy in the combustion facility 50 required for recovering CO₂, and to improve energy efficiency in the plant 5 in which the CO₂ recovery unit 53 is applied.

As shown in FIG. 6, in the CO₂ recovery unit 53 according to the third embodiment, an on-off valve 59 b can be provided in the waste heat line 59 a for circulating the heat medium 108. When the on-off valve 59 b is opened, the heat medium 108 is circulated, thereby performing heat exchange between the heat medium 108 and the combustion air 102. On the other hand, when the on-off valve 59 b is closed, the heat medium 108 is not circulated, and thus the heat medium 108 is not heat-exchanged with the combustion air 102.

According to the CO₂ recovery unit 53, for example, when there is a load variation in at least one of the plant 5 and the CO₂ recovery unit 53, the heat exchange amount in the air preheater 59 can be adjusted by operating the on-off valve 59 b. Accordingly, a stable operation can be performed even at the time of the load variation.

The CO₂ recovery method according to the third embodiment includes the air preheating step of preheating the combustion air 102 before reaching the combustion facility 50 by waste heat discharged in the process of recovering CO₂.

According to the CO₂ recovery method, the combustion air 102 is preheated by using waste heat discharged in the process of recovering CO₂. Therefore, the temperature of the flue gas 101 discharged from the boiler in the combustion facility 50 rises, thereby increasing the heat exchange amount in the condensed water/flue gas heat exchanger 57. As a result, the temperature of the condensed water 106 a returned from the regenerating heater 32 to the combustion facility 50 rises, thereby enabling to reduce consumption energy in the combustion facility 50 required for recovering CO₂, and to improve energy efficiency in the plant 5 in which the CO₂ recovery unit 53 is applied.

As shown in FIG. 6, the CO₂ recovery method according to the third embodiment further includes a non-heat exchanging step of stopping the heat exchange at the air preheating step by closing the on-off valve 59 b.

According to the CO₂ recovery method, for example, when there is a load variation in at least one of the plant 5 and the CO₂ recovery unit 53, the heat exchange amount at the air preheating step can be adjusted by operating the on-off valve 59 b. Accordingly, a stable operation can be performed even at the time of the load variation.

In FIG. 6, which explains the present embodiment, a configuration including the air preheater 59 (air preheating step) is shown with respect to the configuration shown in FIG. 3, which explains the first embodiment. However, the air preheater 59 (air preheating step) can be provided in the configuration shown in FIG. 1, which explains the first embodiment.

Furthermore, the configuration of the present embodiment can be a configuration included in the second embodiment.

[Fourth Embodiment]

A fourth embodiment of the present invention is explained with reference to the drawings. FIG. 7 is a schematic diagram of a plant in which a CO₂ recovery unit according to the fourth embodiment is applied.

The CO₂ recovery unit 53 according to the present embodiment includes the condensed water/flue gas heat exchanger 57 (in a CO₂ recovery method, condensed water/flue gas heat exchanging step), similarly to the CO₂ recovery unit 53 according to the first embodiment. The CO₂ recovery unit 53 further includes an air preheater 60 (in the CO₂ recovery method, air preheating step). Therefore, in the fourth embodiment, a configuration of the air preheater 60 (in the CO₂ recovery method, air preheating step) is explained, and elements equivalent to those in the first embodiment described above are denoted by like reference signs and explanations thereof will be omitted.

As shown in FIG. 7, the air preheater 60 has a condensed water/combustion air heat exchanging line 60 a. The condensed water/combustion air heat exchanging line 60 a is placed in the condensed water line 32 c, and extended to the air line 56 in an upstream of air of the air/flue gas heat exchanger 55, so that the combustion air 102 in the air line 56 is preheated by heat-exchanging it with the condensed water 106 a to be returned from the regenerating heater 32 to the combustion facility 50. Furthermore, the condensed water/flue gas heat exchanger 57 is formed in the condensed water line 32 c passing through the air preheater 60.

As described above, the CO₂ recovery unit 53 according to the fourth embodiment includes the air preheater 60 that preheats the combustion air 102 before reaching the combustion facility 50 by the condensed water 106 a before reaching the condensed water/flue gas heat exchanger 57.

According to the CO₂ recovery unit 53, the combustion air 102 is preheated by using the condensed water 106 a before reaching the condensed water/flue gas heat exchanger 57. Therefore, the temperature of the flue gas 101 discharged from the boiler in the combustion facility 50 rises, thereby increasing the heat exchange amount in the condensed water/flue gas heat exchanger 57. As a result, the temperature of the condensed water 106 a returned from the regenerating heater 32 to the combustion facility 50 increases, thereby enabling to reduce consumption energy in the combustion facility 50 required for recovering CO₂, and to improve energy efficiency in the plant 5 in which the CO₂ recovery unit 53 is applied.

In the CO₂ recovery unit 53 according to the fourth embodiment, a bypass line 60 b that directly connects the condensed water line 32 c without via the condensed water/combustion air heat exchanging line 60 a is provided in the condensed water line 32 c for returning the condensed water 106 a from the regenerating heater 32 to the combustion facility 50. Furthermore, an on-off valve 60 c is provided on a downstream side of the condensed water/combustion air heat exchanging line 60 a for feeding the condensed water 106 a to the air preheater 60. Further, an on-off valve 60 d is provided in the bypass line 60 b.

When heat exchange between the condensed water 106 a and the combustion air 102 is to be performed by the air preheater 60, the on-off valve 60 c is opened and the on-off valve 60 d is closed. With this configuration, the condensed water 106 a in the process of being returned to the combustion facility 50 via the condensed water line 32 c passes through the condensed water/combustion air heat exchanging line 60 a. Therefore, heat exchange between the condensed water 106 a and the combustion air 102 is performed in the air preheater 60.

On the other hand, when heat exchange between the condensed water 106 a and the combustion air 102 is not performed in the air preheater 60, the on-off valve 60 c is closed, and the on-off valve 60 d is opened. With this configuration, the condensed water 106 a in the process of being returned to the combustion facility 50 via the condensed water line 32 c is returned to the combustion facility 50 without via the condensed water/combustion air heat exchanging line 60 a. Therefore, heat exchange between the condensed water 106 a and the combustion air 102 is not performed in the air preheater 60 (non-heat exchanging step).

As described above, in the CO₂ recovery unit 53 according to the fourth embodiment, the condensed water/combustion air heat exchanging line 60 a for performing heat exchange between the condensed water 106 a and the combustion air 102 is provided in the middle of the condensed water line 32 c for returning the condensed water 106 a from the regenerating heater 32 to the combustion facility 50, and the bypass line 60 b for directly connecting the condensed water line 32 c without via the condensed water/combustion air heat exchanging line 60 a is provided.

According to the CO₂ recovery unit 53, for example, when there is a load variation in at least one of the plant 5 and the CO₂ recovery unit 53, the heat exchange amount between the condensed water 106 a and the combustion air 102 in the air preheater 60 can be adjusted by the bypass line 60 b. Accordingly, a stable operation can be performed even at the time of the load variation.

The CO₂ recovery method according to the fourth embodiment includes the air preheating step of preheating the combustion air 102 before reaching the combustion facility 50 by the condensed water 106 a, before performing the condensed water/flue gas heat exchanging step.

According to the CO₂ recovery method, the combustion air 102 is preheated by using the condensed water 106 a before reaching the condensed water/flue gas heat exchanging step. Therefore, the temperature of the flue gas 101 discharged from the boiler in the combustion facility 50 rises, thereby increasing the heat exchange amount in the condensed water/flue gas heat exchanger 57. As a result, the temperature of the condensed water 106 a returned from the regenerating heater 32 to the combustion facility 50 rises, thereby enabling to reduce consumption energy in the combustion facility 50 required for recovering CO₂, and to improve energy efficiency in the plant 5 in which the CO₂ recovery unit 53 is applied.

The CO₂ recovery method according to the fourth embodiment includes the non-heat exchanging step of returning the condensed water 106 a to the combustion facility 50 without via the air preheating step.

According to the CO₂ recovery method, for example, when there is a load variation in at least one of the plant 5 and the CO₂ recovery unit 53, the heat exchange amount between the condensed water 106 a and the flue gas 101 at the condensed water/flue gas heat exchanging step can be adjusted by the non-heat exchanging step. Accordingly, a stable operation can be performed even at the time of the load variation.

In FIG. 7, which explains the present embodiment, a configuration including the air preheater 60 (air preheating step) is shown with respect to the configuration shown in FIG. 3, which explains the first embodiment. However, the air preheater 60 (air preheating step) can be provided in the configuration shown in FIG. 1, which explains the first embodiment.

Furthermore, the configuration of the present embodiment can be a configuration included in the second embodiment.

EXAMPLES

Examples showing effects of the present invention are explained below, while the present invention is not limited thereto. FIG. 8 depicts a power output reduction rate of a process in which the method of the present invention is applied to a coal-combustion thermal power generating facility with a generating capacity of 900 megawatts.

As a comparative example, a conventional technique in which any condensed water/flue gas heat exchanger is not provided and condensed water is directly returned to a combustion facility is exemplified as a comparative example 1. An Example 1 has the configuration of the first embodiment shown in FIGS. 1 to 3. An Example 2 has the configuration of the second embodiment shown in FIGS. 4 and 5. An Example 3 has the configuration of the third embodiment shown in FIG. 6. An Example 4 has the configuration of the fourth embodiment shown in FIG. 7.

Positions at an outlet of the CO₂ recovery unit (1), a condensed water outlet of the air preheater (9), a condensed water inlet of the combustion facility (2), a flue gas inlet of the air preheater (10), an air inlet of the air/flue gas heat exchanger (3), an air inlet of the combustion facility (4), a flue gas outlet of the combustion facility (5), a flue gas inlet of the condensed water/flue gas heat exchanger (6), a flue gas outlet of the condensed water/flue gas heat exchanger (7), and a flue gas outlet of the circulating water/flue gas heat exchanger (8) shown in FIG. 8 are indicated by like numbers in brackets in FIG. 1, FIG. 3, FIG. 4, FIG. 6, and FIG. 7 corresponding to each of the Examples.

Because the comparative example 1 does not include the condensed water/flue gas heat exchanger, the condensed water temperature at the outlet of the CO₂ recovery unit (1) and that at the condensed water inlet of the combustion facility (2) are both 100[° C.], and therefore the power output becomes 791 [MW]. The reduction in the power output in the comparative example 1 is 12.1%.

On the other hand, because the Example 1 includes the condensed water/flue gas heat exchanger 57, the condensed water temperature at the condensed water inlet of the combustion facility (2) is heated to 126[° C.] with respect to the condensed water temperature 100[° C.] at the outlet of the CO₂ recovery unit (1). Accordingly, the reduction in the power output was smaller than that in the comparative example 1, and was 11.6%.

The Example 2 includes the circulating water/flue gas heat exchanger 58 a and the circulating water/absorbent heat exchanger 58 b, in addition to the condensed water/flue gas heat exchanger 57. Therefore, the condensed water temperature at the condensed water inlet of the combustion facility (2) was heated to 126[° C.] with respect to the condensed water temperature 100[° C.] at the outlet of the CO₂ recovery unit (1), and the rich solution 104 b of the absorbent 104 was heated to 93.8[° C.] by the circulating water/flue gas heat exchanger 58 a and the circulating water/absorbent heat exchanger 58 b. Accordingly, the reduction in the power output was smaller than that in the comparative example 1, and was 11.3%.

The Example 3 includes the air preheater 59 according to the third embodiment shown in FIG. 6, in addition to the condensed water/flue gas heat exchanger 57. Therefore, the condensed water temperature at the condensed water inlet of the combustion facility (2) was heated to 154[° C.] with respect to the condensed water temperature 100[° C.] at the outlet of the CO₂ recovery unit (1). Accordingly, the reduction in the power output was smaller than that in the comparative example 1, and was 10.8%.

The Example 4 includes the air preheater 60 according to the fourth embodiment shown in FIG. 7, in addition to the condensed water/flue gas heat exchanger 57. Therefore, the condensed water temperature at the condensed water inlet of the combustion facility (2) was heated to 157[° C.] with respect to the condensed water temperature 100[° C.] at the outlet of the CO₂ recovery unit (1). Accordingly, the reduction in the power output was smaller than that in the comparative example 1, and was 10.8%.

As a result, as shown in FIG. 8, according to these Examples, it can be understood that energy efficiency in the combustion facility can be improved because the power output is improved.

REFERENCE SIGNS LIST

1 cooling column

1 e cooler

2 absorber

22 f cooler

3 regenerator

31 absorbent regenerating unit

31 e cooler

32 regenerating heater

32 a heating line

32 b steam extracting line

32 c condensed water line

33 CO₂ recovering unit

33 b cooler

34 lean solution/condensed water heat recovery unit

4 rich/lean heat exchanger

5 plant

50 combustion facility

51 flue gas duct

52 desulfurizer

53 CO₂ recovery unit

54 stack

55 air/flue gas heat exchanger

56 air line

57 condensed water/flue gas heat exchanger

58 a circulating water/flue gas heat exchanger

58 b circulating water/absorbent heat exchanger

59 air preheater

60 air preheater

101 flue gas

101 a emission gas

102 combustion air

103 cooling water

104 absorbent

104 a lean solution

104 b rich solution

105 wash water

106 steam

106 a condensed water

107 circulating water

108 heat medium 

The invention claimed is:
 1. A plant comprising: a combustion facility that discharges flue gas to a flue gas duct and heats condensed water from a condensed water line so as to discharge the heated condensed water to a steam extracting line as steam; an air/flue gas heat exchanger that heat-exchanges the flue gas with combustion air; a CO₂ recovery including: an absorber that reduces CO₂ in flue gas discharged from the combustion facility via the air/flue gas heat exchanger by absorbing CO₂ by an absorbent; a regenerator that heats the absorbent having absorbed CO₂ to emit CO₂, and regenerates and supplies the absorbent to the absorber; and a regenerating heater that heats the absorbent in the regenerator with the steam from the steam extracting line and returns heated condensed water to the combustion facility via the condensed water line; and a condensed water/flue gas heat exchanger that heats the condensed water of the condensed water line by heat-exchanging the condensed water with the flue gas in the flue gas duct discharged from the air/flue gas heat exchanger.
 2. The plant according to claim 1, wherein a condensed water/flue gas heat exchanging line for heat-exchanging between the condensed water and the flue gas is provided in middle of the condensed water line, and a bypass line for directly connecting the condensed water line without via the condensed water/flue gas heat exchanging line is provided.
 3. The plant according to claim 1, further comprising: a circulating water/flue gas heat exchanger that performs heat exchange between circulating water and flue gas in a flue gas duct in the combustion facility, at a downstream of flue gas of the condensed water/flue gas heat exchanger; and a circulating water/absorbent heat exchanger that performs heat exchange between an absorbent having absorbed CO₂ in the absorber and the circulating water before the absorbent reaches the regenerator.
 4. The plant according to claim 1, further comprising an air preheater that preheats combustion air before reaching the combustion facility by waste heat discharged in a process of recovering CO₂.
 5. The plant according to claim 1 further comprising an air preheater that preheats combustion air before reaching the combustion facility by the condensed water before reaching the condensed water/flue gas heat exchanger. 